EP1035391B1 - Procédé et installation de purification et de séparation d'air par voie cryogénique sans pré-refroidissement - Google Patents
Procédé et installation de purification et de séparation d'air par voie cryogénique sans pré-refroidissement Download PDFInfo
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- EP1035391B1 EP1035391B1 EP00400236A EP00400236A EP1035391B1 EP 1035391 B1 EP1035391 B1 EP 1035391B1 EP 00400236 A EP00400236 A EP 00400236A EP 00400236 A EP00400236 A EP 00400236A EP 1035391 B1 EP1035391 B1 EP 1035391B1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/104—Alumina
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/25—Coated, impregnated or composite adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/416—Further details for adsorption processes and devices involving cryogenic temperature treatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/12—Particular process parameters like pressure, temperature, ratios
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Definitions
- the present invention relates to air separation methods atmospheric by cryogenic distillation improved with elimination of impurities by adsorption, prior to said distillation.
- atmospheric air contains compounds or impurities to be removed before any cryogenic separation of the air, that is to say prior to the introduction of air into the exchangers thermal of the cold box of an air separation unit.
- This air pre-treatment is usually called air cleaning or "header" purification because carried out upstream of the separation unit cryogenic.
- air pretreatment is carried out, as the case may be, by TSA (Temperature Swing Adsorption) or PSA process (Pressure Swing Adsorption).
- TSA Temporal Swing Adsorption
- PSA Pressure Swing Adsorption
- a PSA process cycle includes, substantially the same steps a), b) and e), but differs from a process TSA by an absence of heating of the waste gas (es) during the regeneration step (step c)), therefore the absence of step d) and, in generally a shorter cycle time than in the TSA process.
- the air pre-treatment devices include at least two adsorbers, operating in parallel, i.e. alternately, one of the adsorbers being in the production phase, while the other is in the regeneration phase.
- TSA or PSA air purification processes are in particular described in documents US-A-3,738,084, US-A-5,531,808, US-A-5,587,003 and US-A-4,233,038.
- the efficiency of air prepurification is clearly favored for low temperatures, i.e. temperatures close to 5 ° C, or even more for clearly temperatures lower.
- the air freed from all or part of its harmful impurities, in particular of the CO 2 and H 2 O type is then conventionally cooled to cryogenic temperature, i.e. in general to a temperature below about -120 ° C, before being conveyed to the cryogenic distillation unit and introduced into one or more distillation columns for the purpose of '' be separated to recover nitrogen, oxygen and / or argon.
- cryogenic temperature i.e. in general to a temperature below about -120 ° C
- This step of pre-cooling the air increases notably the overall investment, complicates the process, can pose reliability problems and therefore leads to an additional cost of the installation, being given that it is then necessary to provide means for pre-cooling, such as heat exchangers or the like, i.e. a refrigeration unit.
- the aim of the present invention is to alleviate the problems and disadvantages mentioned above by proposing an air separation method cryogenic not requiring pre-cooling of the air by a refrigeration unit, before its introduction into the adsorber (s) the header purification unit, i.e. a process of air separation by cryogenic route simplified compared to existing processes.
- the air is subjected to a pre-cooling step by the refrigeration system 2 before its purification by adsorption in the adsorbers 3a or 3b, operating in parallel.
- FIG. 2 represents, on the other hand, a diagram of an installation of air separation by cryogenic means according to the present invention, which is similar to that of FIG. 1, except that, in this case, the refrigeration system 2 has been removed.
- the air is sent directly, after compression and possibly adjustment (in 7) of its temperature to a temperature of at least + 15 ° C, preferably from +25 to + 50 ° C, in at minus one of the adsorbers 3a and 3b to be pretreated there before being cooled at cryogenic temperature and separated by cryogenic distillation as previously.
- the inventors have demonstrated, as shown in the table below, that in order to achieve effective adsorption of the impurities contained in the air, in the absence of the pre-cooling step by refrigeration system 2 before adsorption, it is necessary to significantly increase the air adsorption pressure, that is to say to purify the air in the adsorbers 3a and 3b at a pressure of at least 11.4.10 5 Pa, preferably at least 15.10 5 Pa and up to 40.10 5 Pa.
- This increase in pressure makes it possible, on the one hand, to reduce the water vapor content of the air flow and, on the other hand, promote adsorption impurities in the air by increasing their partial pressure.
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- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
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- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Separation Of Gases By Adsorption (AREA)
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Description
- après distillation cryogénique, on récupère au moins un composé choisi parmi l'azote, l'oxygène, l'argon ou leurs mélanges. Le ou les composés ainsi produits peuvent être de pureté variable et, de préférence, on récupère au moins l'un de ces composés sous forme liquide pour valoriser l'énergie apportée par l'augmentation de la pression de l'air.
- à l'étape (c), l'adsorption est opérée à une pression de 21.105 Pa à 40.105 Pa, avantageusement de 22.105 Pa à 38.105 Pa.
- à l'étape (a), la compression est opérée à une pression de 21.105 Pa à 40.105 Pa, avantageusement de 22.105 Pa à 38.105 Pa.
- à l'étape (b), l'air introduit dans le récipient d'adsorption est à une température d'adsorption d'au moins +21 °C, de préférence de +25°C à +65°C, avantageusement de +30°C à +50°C. Lorsque l'air en sortie de compression est à une température trop élevée, par exemple +80°C, on lui fait subir un refroidissement pour l'amener dans une plage de température du procédé selon l'invention mais, de toute façon, à une température d'au moins +15°C. En d'autres termes, optionnellement, le procédé de l'invention peut comprendre une étape complémentaire d'ajustage de la température de l'air, subséquente à l'étape (a) et préalable à l'étape (b), mais sans pour autant constituer une étape de pré-refroidissement classique par un groupe frigorifique. Avantageusement, cette étape complémentaire d'ajustage de la température de l'air consiste simplement à diminuer la température de l'air par échange thermique au moyen d'un ou plusieurs échangeurs de chaleur, de préférence des échangeurs dans lesquels .circule de l'eau.
- à l'étape (c), les impuretés adsorbées sont choisies dans le groupe formé par le dioxyde de carbone, la vapeur d'eau, les oxydes d'azote, les oxydes de soufre et les hydrocarbures.
- l'adsorbant est choisi parmi les zéolites, les alumines, les gels de silice et leurs mélanges.
- la distillation cryogénique de l'étape (e) est opérée à une pression de 105 Pa à 30.105 Pa, de préférence de l'ordre de 1,3.105 Pa à 20.105 Pa.
- il comporte une étape de régénération de l'adsorbant à une température de régénération comprise entre 100°C et 280°C. De manière connue en soi, l'adsorbant subit cycliquement une régénération par chauffage à la température de régénération par balayage des particules d'adsorbant avec un gaz choisi parmi l'azote ou un mélange d'azote et d'oxygène.
- la pression de régénération est comprise entre 1.105 Pa et 30.105 Pa.
- les particules d'adsorbant sont choisies parmi les particules de zéolite de type faujasite, X, LSX, A, mordénite ou leurs mélanges, de préférence les particules de zéolite sont de type X ou LSX ayant un rapport Si/Al ≤1.15, de préférence d'environ 1.
- les particules d'adsorbant sont choisies parmi les particules d'alumine activée et d'alumine imprégnée.
- au moins un adsorbeur contient au moins un lit ou au moins une couche de particules de zéolite et au moins un lit ou au moins une couche de particules d'alumine, de préférence au moins un lit ou au moins une couche de particules d'alumine est situé en amont d'au moins un lit ou au moins une couche de particules de zéolite par rapport au sens de circulation de l'air.
- comprimé par un compresseur 1, par exemple du type à refroidissement à eau,
- légèrement ajusté en température par un échangeur thermique 7 à circulation d'eau,
- pré-refroidi par un groupe frigorifique ou système de réfrigération 2 jusqu'à une température de l'ordre de +5°C, voire même inférieure à +5°C,
- introduit dans l'un ou l'autre des adsorbeurs 3a et 3b pour y être purifié par adsorption desdites impuretés sur un ou plusieurs lits d'adsorbant, par exemple une adsorbant de type zéolite,
- refroidi à une température cryogénique, par exemple à -170°C, dans une boíte froide 4 contenant un ou plusieurs échangeurs thermiques,
- puis séparé par distillation cryogénique dans une ou plusieurs colonnes 5 de distillation cryogénique en vue de produire de l'azote et/ou de l'oxygène notamment sous forme liquide et/ou gazeuse.
Essais | Avec pré-refroidissement | Sans pré-refroidissement | Sans pré-refroidissement |
Débit d'adsorption (Nm 3 /h) | 50 000 | 50 000 | 50 000 |
Température d'adsorption | 10°C | 35°C | 35°C |
Pression d'adsorption | 6.10 5 Pa (art antérieur) | 6.10 5 Pa (art antérieur) | 30.10 5 Pa (invention) |
Débit de régénération (Nm 3 /h) | 10 000 | 24 000 | 10 000 |
Température de régénération | 150°C | 150°C | 150°C |
Pression de régénération | 1,1.10 5 Pa | 1,1.10 5 Pa | 1,1.10 5 Pa |
Temps de cycle (minutes) | 150 | 250 | 200 |
Masse d'adsorbant | 8 900 kg | 51 000 kg | 13 500 kg |
Claims (10)
- Procédé de séparation cryogénique d'air contenant des impuretés, dans lequel on procède selon les étapes de :(a) compression d'air à séparer à une pression d'au moins 21.105 Pa,(b) introduction de l'air à une pression d'au moins 21.105 Pa, dans l'un ou l'autre des deux récipients d'adsorption fonctionnant en parallèle et contenant chacun des particules d'au moins un adsorbant,(c) adsorption d'au moins une partie des impuretés contenues dans l'air sur lesdites particules d'adsorbant, à une pression d'au moins 21.105 Pa, à un débit d'adsorption compris entre 250 Nm3/h et 106 Nm3/h, et selon un cycle de type Temperature Swing Adsorption (TSA), et(d) refroidissement de l'air purifié à l'étape (c) jusqu'à une température cryogénique inférieure à -120°C,(e) distillation cryogénique de l'air refroidi à l'étape (d),
dans lequel l'air comprimé n'est pas soumis à un pré-refroidissement subséquemment à l'étape (a) et préalablement à l'étape (b), et
comportant, en outre, une étape cyclique de régénération de l'adsorbant par balayage avec un gaz de régénération ayant une température de régénération comprise entre 40°C et 350°C, et à un débit de régénération allant de 5 à 70% du débit d'adsorption. - Procédé selon la revendication 1, caractérisé en ce qu'à l'étape (c), l'adsorption est opérée à une pression de 21.105 Pa à 40.105 Pa
- Procédé selon l'une des revendications 1 ou 2, caractérisé en ce qu'à l'étape (c), l'adsorption est opérée à une pression de 22.105 Pa à 38.105 Pa.
- Procédé selon l'une des revendications 1 ou 2, caractérisé en ce qu'à l'étape (a), l'air est comprimé à une pression d'au moins 21.105 Pa à 40.105 Pa, préférentiellement de 22.105 Pa à 38.105 Pa.
- Procédé selon l'une des revendications 1 à 4, caractérisé en ce qu'à l'étape (b), l'air introduit dans le récipient d'adsorption est à une température d'adsorption d'au moins +21 °C, de préférence de +25°C à +65°C, préférentiellement de +30°C à +50°C.
- Procédé selon l'une des revendications 1 à 5, caractérisé en ce qu'à l'étape (c), les impuretés adsorbées sont choisies dans le groupe formé par le dioxyde de carbone, la vapeur d'eau, les oxydes d'azote, les oxydes de soufre et les hydrocarbures.
- Procédé selon l'une des revendications 1 à 6, caractérisé en ce l'adsorbant est choisi parmi les zéolites, les alumines, les gels de silice et leurs mélanges.
- Procédé selon l'une des revendications 1 à 7, caractérisé en ce qu'il comporte, subséquemment à l'étape (a) et préalablement à l'étape (b), une étape complémentaire d'ajustage de la température de l'air à une valeur d'au moins +15°C, de préférence comprise entre +30°C et +50°C.
- Procédé selon la revendication 8, caractérisé en ce que l'ajustage de température est réalisé au moyen d'au moins un échangeur à eau.
- Procédé selon la revendication 1, caractérisé en ce que le gaz de régénération est choisi parmi l'azote ou un mélange d'azote et d'oxygène.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9903064 | 1999-03-12 | ||
FR9903064A FR2790823B1 (fr) | 1999-03-12 | 1999-03-12 | Procede et installation de purification et de separation d'air par voie cryogenique sans pre-refroidissement |
Publications (2)
Publication Number | Publication Date |
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EP1035391A1 EP1035391A1 (fr) | 2000-09-13 |
EP1035391B1 true EP1035391B1 (fr) | 2004-03-24 |
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Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP00400236A Revoked EP1035391B1 (fr) | 1999-03-12 | 2000-01-31 | Procédé et installation de purification et de séparation d'air par voie cryogénique sans pré-refroidissement |
Country Status (8)
Country | Link |
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US (1) | US6240745B1 (fr) |
EP (1) | EP1035391B1 (fr) |
JP (1) | JP2000271425A (fr) |
AT (1) | ATE262667T1 (fr) |
CA (1) | CA2298125A1 (fr) |
DE (1) | DE60009186T2 (fr) |
ES (1) | ES2216831T3 (fr) |
FR (1) | FR2790823B1 (fr) |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2830463B1 (fr) | 2001-10-09 | 2004-08-06 | Air Liquide | Procede et appareil de traitement d'un gaz par adsorption, notamment d'epuration d'air atmospherique avant separation par distillation |
FR2896861B1 (fr) * | 2006-01-31 | 2008-07-18 | Air Liquide | Procede de regulation d'un ensemble d'appareils de separation d'air par distillation cryogenique et ensemble d'appareils de separation d'air operant selon ledit procede |
FR2918579B1 (fr) * | 2007-07-13 | 2010-01-01 | Air Liquide | Procede de purification d'un gaz contenant du co2 par integration d'unite de purification par adsorption |
DE102010020283A1 (de) * | 2010-05-12 | 2011-11-17 | Linde Aktiengesellschaft | Adsorptionsverfahren |
EP3449997A1 (fr) * | 2017-08-28 | 2019-03-06 | Casale Sa | Processus d'adsorption à oscillation de température |
CN109173620A (zh) * | 2018-08-17 | 2019-01-11 | 邯郸钢铁集团有限责任公司 | 一种可以降低能耗的压缩空气干燥器 |
US20220040673A1 (en) * | 2018-09-25 | 2022-02-10 | Sekisui Chemical Co., Ltd. | Method for reusing zeolite adsorbent and regenerated adsorbent |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS54103778A (en) * | 1978-02-03 | 1979-08-15 | Hitachi Ltd | Air separator pretreatment and apparatus therefor |
US4249915A (en) * | 1979-05-30 | 1981-02-10 | Air Products And Chemicals, Inc. | Removal of water and carbon dioxide from air |
EP0175791B1 (fr) * | 1984-03-29 | 1988-11-09 | Daidousanso Co., Ltd. | Installation de production d'azote gazeux de grande purete |
US5463869A (en) * | 1994-08-12 | 1995-11-07 | Air Products And Chemicals, Inc. | Integrated adsorption/cryogenic distillation process for the separation of an air feed |
FR2728663B1 (fr) * | 1994-12-23 | 1997-01-24 | Air Liquide | Procede de separation d'un melange gazeux par distillation cryogenique |
US5587003A (en) * | 1995-03-21 | 1996-12-24 | The Boc Group, Inc. | Removal of carbon dioxide from gas streams |
JP3416391B2 (ja) * | 1995-05-25 | 2003-06-16 | 日本酸素株式会社 | 空気液化分離装置の前処理方法及び装置 |
US5701763A (en) * | 1997-01-07 | 1997-12-30 | Praxair Technology, Inc. | Cryogenic hybrid system for producing low purity oxygen and high purity nitrogen |
US5802872A (en) * | 1997-07-30 | 1998-09-08 | Praxair Technology, Inc. | Cryogenic air separation with combined prepurifier and regenerators |
-
1999
- 1999-03-12 FR FR9903064A patent/FR2790823B1/fr not_active Expired - Fee Related
-
2000
- 2000-01-31 ES ES00400236T patent/ES2216831T3/es not_active Expired - Lifetime
- 2000-01-31 EP EP00400236A patent/EP1035391B1/fr not_active Revoked
- 2000-01-31 DE DE60009186T patent/DE60009186T2/de not_active Expired - Fee Related
- 2000-01-31 AT AT00400236T patent/ATE262667T1/de not_active IP Right Cessation
- 2000-02-08 CA CA002298125A patent/CA2298125A1/fr not_active Abandoned
- 2000-02-14 US US09/503,182 patent/US6240745B1/en not_active Expired - Fee Related
- 2000-03-10 JP JP2000066547A patent/JP2000271425A/ja active Pending
Also Published As
Publication number | Publication date |
---|---|
FR2790823A1 (fr) | 2000-09-15 |
ES2216831T3 (es) | 2004-11-01 |
US6240745B1 (en) | 2001-06-05 |
ATE262667T1 (de) | 2004-04-15 |
DE60009186D1 (de) | 2004-04-29 |
JP2000271425A (ja) | 2000-10-03 |
CA2298125A1 (fr) | 2000-09-12 |
DE60009186T2 (de) | 2005-02-24 |
FR2790823B1 (fr) | 2001-06-15 |
EP1035391A1 (fr) | 2000-09-13 |
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